EP1053783A1 - Circulant reacteur en lit - Google Patents

Circulant reacteur en lit Download PDF

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Publication number
EP1053783A1
EP1053783A1 EP00660099A EP00660099A EP1053783A1 EP 1053783 A1 EP1053783 A1 EP 1053783A1 EP 00660099 A EP00660099 A EP 00660099A EP 00660099 A EP00660099 A EP 00660099A EP 1053783 A1 EP1053783 A1 EP 1053783A1
Authority
EP
European Patent Office
Prior art keywords
riser
bed reactor
fluidized bed
channel
cyclone
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP00660099A
Other languages
German (de)
English (en)
Other versions
EP1053783B1 (fr
Inventor
Seppo Ruottu
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ruottu Seppo
Original Assignee
Einco Oy
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Filing date
Publication date
Application filed by Einco Oy filed Critical Einco Oy
Publication of EP1053783A1 publication Critical patent/EP1053783A1/fr
Application granted granted Critical
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Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
    • F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
    • F26B3/092—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed agitating the fluidised bed, e.g. by vibrating or pulsating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
    • B01J8/1854—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement inside the reactor to form a loop
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1872—Details of the fluidised bed reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C2003/006—Construction of elements by which the vortex flow is generated or degenerated

Definitions

  • the present invention concerns a circulating fluidized bed reactor according to the preamble of claim 1.
  • a “Circulating Fluidized Bed (CFB) Reactor” stands for a multiphase flow apparatus formed by gas distribution nozzles, a riser i.e. a riser tube, a cyclone separator and a straight, unregulated return channel, a substantial part of the particles being conducted through the cyclone and returned from the cyclone to the lower part of the riser.
  • Second generation CFB reactors The constructions created as a result of this thinking can be called second generation CFB reactors.
  • Horizontal CFB boilers having quadrical cross section and employing cooled multi-inlet cyclones can, e.g., be mentioned as examples of second generation CFB reactors. All of these had in common that the whole construction was cooled and the protective materials were primarily used only for protection against wear. In small boilers also other part of the boiler had to be provided with insulation masses in order to prevent excessive cooling.
  • the second generation CFB reactors were poorly applicable to any other use than as steam boilers. In the process, chemical and oil refining industry the reactors are expected to meet requirements on reaction, heat and flow technique rather than constructional technical features. As a result, a new phase of the development work was initiated in the 1990's with the aim of providing multi-inlet, concentrical CFB reactor technology with numerous applications. Since the starting point of the this development phase was formed by the second generation CFB reactors, it is possible to talk about already the third generation CFB reactors.
  • the third generation CFB reactors are characterized by a multi-inlet cyclone fitted concentrically inside the riser.
  • the circulating fluidized bed reactor generally comprises an elongated riser which has an at least essentially vertical central axis, feed nozzles fitted at the lower part of the riser for feeding solid matter and fluidization gas into the riser and a separation unit fitted at the upper part of the riser for separation of solids from the fluidization gas.
  • the separation unit preferably consists of a multi-inlet cyclone, comprising a separation chamber with guide vanes for bringing the gas which is being treated into a gas flow directed along the inner surface of the separation chamber for separating the solid matter from the gas mainly under the influence of centrifugal force and a dipleg (returm channel) for recovering the solids.
  • the multi-inlet cyclone and the return channel are fitted annularly outside the riser.
  • a fourth generation CFB reactor is provided which is both fuctionally and constructively entirely different from the third generation CFB reactors.
  • the CFB reactor according to the present invention is characterized by what is stated in the characterizing part of claim 1.
  • the invention provides considerable advantages. Thus, its most central benefits in comparison to all prior CFB reactor types is that it removes the earlier limitation that the ratio of the height to the diameter should be in practice greater than 1. In the device according to the invention said ratio can be 1 or smaller, e.g. about 0.1 to 0.95.
  • the flow dynamics of the present solution are beneficial because both the friction of the gas and the centrifugal force drive the particles obtained from the riser channel towards the wall of the cyclone.
  • two separate interconnected CFB are used (e.g. a reactor and a regenerator), catalyst exchange between the reactors is easier to accomplish with fourth generation CFB reactors.
  • the use of two separate CFB reactors may be more advantageous that the use of a nested construction when the amount of solids which should be changed is small in comparison to the amount of internal recirculation of the reactors.
  • the CFB reactor according to the embodiment of Figure 1 comprises a feed nozzle 1 for fluidization gas, a distribution box 2, a baffle plate 3, an elongated riser channel 5, which has an essentially vertical central axis having a lower portion 4 and a top portion in which there is fitted a separation unit.
  • the separation unit preferably comprises a multi-inlet cyclone 6 - 11, with a set of cyclone vanes 6, an annular cyclone chamber 7, an annular central pipe 8, a connection cone 9, a return channel 10 and a gas outlet nozzle 11.
  • the circulating fluidized bed reactor is operated as follows: Fluidization gas fed from the distribution box 2 via the feed nozzle 1 is conducted through the baffle plate 3 to the lower portion 4 of the riser, wherein the gas and the fluidized particles are mixed. A substantial part of the fluidized particles is conducted with the gas to the riser 4 and further together with the gas to a set of cyclone vanes 6 fitted on the periphery of the upper portion of the riser. The top view of the set of vanes is shown in Figure 1d. From the set of vanes 6 the gas and the particles are conducted to the cyclone chamber 7 fitted annularly around the riser. The central tube 8 of the cyclone is also fitted annularly about the riser.
  • the gases are conducted via nozzle 11 out of the CFB reactor.
  • the flow from the cyclone chamber is brought into a rotating movement in the set of vanes 6 and, as a resultof the movement, the particles are carried to the wall of the cyclone chamber 7 and fall into the connection cone 9 of the cyclone chamber 7 and the return channel 10. From the connection cone the particles fall further under the influence of gravity via the return channel 10 back to the lower portion 4 of the riser. As will appear from the drawing, the return channel is fitted about the riser channel.
  • reference numeral 12 designates the top view of the set of cyclone vanes.
  • the vanes which preferably are curved form a plurality (preferably 12 to 40) channels which give the flow which is directed from the inner periphery to the outer periphery of the vanes a vortex having the direction of the perimeter.
  • the flow direction in the set of vanes is changed from against the radius to toward the radius. This, in its turn, gives the functional benefit that in according to the invention both gas friction and the centrifugal force carry the particles against the cyclone wall.
  • the centrifugal force carries the particles against the wall but the gas friction drives them from the wall outwards. In this respect the solution according to the invention is more advantageous.
  • Figure 1 The embodiment of Figure 1 is best suited to applications in which it is deemed appropriate to maintain a constant sectional area of the riser channel.
  • Applications of this kind are exemplified by indirect dryers in which the riser channel is formed by a tubular heat exchanger (reference numeral 14 stands for tubes) of the kind indicated by numerals 13 and 14 in Figures 1b and 1c.
  • Figure 2 shows a second preferred embodiment of a CFB reactor according to the invention.
  • the apparatus includes a feed nozzle 21, a distribution box 22, a baffle plate 23, the lower portion 24 of the riser, a riser 25, a set of cyclone vanes 26, an annular cyclone chamber 27, an annular central tube 28, a connection cone 29, a return channel 30 and a gas outlet nozzle 31.
  • the reactor of Figure 2 differs from the embodiment of Figure 1 in the respect that the diameter of the outer jacket is constant and the cyclone is fitted in the outer jacket of constant diameter by reducing the diameter of the riser in the region of cyclone.
  • This solution is advantageous for, e.g. steam boiler embodiments, in which the outer jacket is formed by a gas-tight tubular panel.
  • a distinct advantage is obtained because in addition to the outer jacket the wall of the riser chamber can be easily constructed from cooled panel walls. Thereby both sides of the wall of the riser chamber and the inner side of the outer wall can be utilized as heat transfer surfaces.
  • the expensive wall panel can be more efficiently utilized and, furthermore, the height of the riser chamber of the boiler is significantly reduced.
  • both investment and operation costs savings can be attained.
  • the return channel can be provided with heat transfer surfaces whereby the heat transfer of the CFB reactor according to the invention can be regulated by the rate of circulating solid matter flow.
  • the return channel can be formed from a plurality of parallel channels.
  • the horizontal section of the CFB reactor according to the invention is most suitably spherical, but within the scope of the same inventive concept it can also be implemented in the horizontal section having various polyhedrical forms.
  • the flow in the central tube 28 and the outlet nozzle 31 can be directed opposite to the directions of Figures 1 and 2.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Drying Of Solid Materials (AREA)
  • Cyclones (AREA)
EP00660099A 1999-05-20 2000-05-22 Circulant reacteur en lit Expired - Lifetime EP1053783B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI991151 1999-05-20
FI991151A FI106242B (fi) 1999-05-20 1999-05-20 Kiertomassareaktori

Publications (2)

Publication Number Publication Date
EP1053783A1 true EP1053783A1 (fr) 2000-11-22
EP1053783B1 EP1053783B1 (fr) 2003-02-26

Family

ID=8554700

Family Applications (1)

Application Number Title Priority Date Filing Date
EP00660099A Expired - Lifetime EP1053783B1 (fr) 1999-05-20 2000-05-22 Circulant reacteur en lit

Country Status (5)

Country Link
US (1) US6467438B1 (fr)
EP (1) EP1053783B1 (fr)
AT (1) ATE233126T1 (fr)
DE (1) DE60001473T2 (fr)
FI (1) FI106242B (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001085872A2 (fr) * 2000-05-04 2001-11-15 Exxonmobil Chemical Patents Inc. Reacteurs a colonne montante
WO2005037422A1 (fr) * 2003-10-21 2005-04-28 Seppo Ruottu Reacteur a lit circulant
US7083762B2 (en) 2002-10-18 2006-08-01 Exxonmobil Chemical Patents Inc. Multiple riser reactor with centralized catalyst return
US7122160B2 (en) 2002-09-24 2006-10-17 Exxonmobil Chemical Patents Inc. Reactor with multiple risers and consolidated transport

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9126174B2 (en) * 2010-03-31 2015-09-08 Uop Llc Hydroprocessing method, or an apparatus relating thereto
FI125978B (fi) 2013-02-22 2016-05-13 Endev Oy Kiertomassakuivuri ja menetelmä märän lietteen kuivaamiseksi
FI125977B (fi) * 2013-02-22 2016-05-13 Endev Oy Menetelmä ja laitteisto lietteen polttamiseksi

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1593520A (en) * 1976-12-08 1981-07-15 Goetaverken Angteknik Ab Fluidized bed reactors
US5070822A (en) * 1990-01-29 1991-12-10 Tampella Power Oy Combustion unit
US5117770A (en) * 1990-01-29 1992-06-02 Tampella Power Oy Combustion unit
WO1998008599A1 (fr) * 1996-08-30 1998-03-05 Neste Oy Dispositif a lit fluidise circulant pour procedes chimiques et physiques
EP0844021A2 (fr) * 1996-11-22 1998-05-27 OMV Aktiengesellschaft Appareil pour la conversion catalytique de substances organiques dans un réacteur à lit fluidisé

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1593520A (en) * 1976-12-08 1981-07-15 Goetaverken Angteknik Ab Fluidized bed reactors
US5070822A (en) * 1990-01-29 1991-12-10 Tampella Power Oy Combustion unit
US5117770A (en) * 1990-01-29 1992-06-02 Tampella Power Oy Combustion unit
WO1998008599A1 (fr) * 1996-08-30 1998-03-05 Neste Oy Dispositif a lit fluidise circulant pour procedes chimiques et physiques
EP0844021A2 (fr) * 1996-11-22 1998-05-27 OMV Aktiengesellschaft Appareil pour la conversion catalytique de substances organiques dans un réacteur à lit fluidisé

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001085872A2 (fr) * 2000-05-04 2001-11-15 Exxonmobil Chemical Patents Inc. Reacteurs a colonne montante
WO2001085872A3 (fr) * 2000-05-04 2002-02-28 Exxonmobil Chem Patents Inc Reacteurs a colonne montante
US7102050B1 (en) 2000-05-04 2006-09-05 Exxonmobil Chemical Patents Inc. Multiple riser reactor
US7195741B2 (en) 2000-05-04 2007-03-27 Exxonmobil Chemical Patents Inc. Multiple riser reactor
US7122160B2 (en) 2002-09-24 2006-10-17 Exxonmobil Chemical Patents Inc. Reactor with multiple risers and consolidated transport
US7083762B2 (en) 2002-10-18 2006-08-01 Exxonmobil Chemical Patents Inc. Multiple riser reactor with centralized catalyst return
US7385099B2 (en) 2002-10-18 2008-06-10 Exxonmobil Chemical Patents Inc. Multiple riser reactor with centralized catalyst return
WO2005037422A1 (fr) * 2003-10-21 2005-04-28 Seppo Ruottu Reacteur a lit circulant

Also Published As

Publication number Publication date
ATE233126T1 (de) 2003-03-15
US6467438B1 (en) 2002-10-22
FI991151A0 (fi) 1999-05-20
EP1053783B1 (fr) 2003-02-26
DE60001473T2 (de) 2003-12-18
DE60001473D1 (de) 2003-04-03
FI106242B (fi) 2000-12-29

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